EP3417035A1 - Verfahren zur entschwefelung eines kohlenwasserstoffgemisches - Google Patents
Verfahren zur entschwefelung eines kohlenwasserstoffgemischesInfo
- Publication number
- EP3417035A1 EP3417035A1 EP17720561.4A EP17720561A EP3417035A1 EP 3417035 A1 EP3417035 A1 EP 3417035A1 EP 17720561 A EP17720561 A EP 17720561A EP 3417035 A1 EP3417035 A1 EP 3417035A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- sodium
- reactor
- hydrocarbon mixture
- dispersion
- desulfurization
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 238000000034 method Methods 0.000 title claims abstract description 70
- 239000000203 mixture Substances 0.000 title claims abstract description 54
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 51
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 51
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 45
- 230000003009 desulfurizing effect Effects 0.000 title abstract 2
- 239000011734 sodium Substances 0.000 claims abstract description 65
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 claims abstract description 64
- 229910052708 sodium Inorganic materials 0.000 claims abstract description 64
- 239000006185 dispersion Substances 0.000 claims abstract description 39
- 238000006243 chemical reaction Methods 0.000 claims abstract description 23
- 150000002898 organic sulfur compounds Chemical class 0.000 claims abstract description 13
- 125000004434 sulfur atom Chemical group 0.000 claims abstract description 3
- 238000006477 desulfuration reaction Methods 0.000 claims description 23
- 230000023556 desulfurization Effects 0.000 claims description 23
- 239000003921 oil Substances 0.000 claims description 19
- 239000002245 particle Substances 0.000 claims description 12
- 239000007791 liquid phase Substances 0.000 claims description 9
- 239000000446 fuel Substances 0.000 claims description 7
- 239000002480 mineral oil Substances 0.000 claims description 6
- 235000010446 mineral oil Nutrition 0.000 claims description 6
- 239000007788 liquid Substances 0.000 claims description 5
- 238000002360 preparation method Methods 0.000 claims description 5
- 238000002156 mixing Methods 0.000 claims description 4
- 238000004519 manufacturing process Methods 0.000 claims description 3
- 238000012545 processing Methods 0.000 claims description 2
- 230000001737 promoting effect Effects 0.000 claims description 2
- 239000007787 solid Substances 0.000 claims description 2
- 230000003068 static effect Effects 0.000 claims description 2
- 239000002699 waste material Substances 0.000 claims description 2
- 238000004140 cleaning Methods 0.000 claims 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 29
- 229910052717 sulfur Inorganic materials 0.000 description 29
- 239000011593 sulfur Substances 0.000 description 29
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 4
- QQONPFPTGQHPMA-UHFFFAOYSA-N Propene Chemical compound CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 4
- 229910052739 hydrogen Inorganic materials 0.000 description 4
- 239000001257 hydrogen Substances 0.000 description 4
- 238000009835 boiling Methods 0.000 description 3
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 2
- 239000000470 constituent Substances 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 150000003464 sulfur compounds Chemical class 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000012512 characterization method Methods 0.000 description 1
- 238000003776 cleavage reaction Methods 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 239000002283 diesel fuel Substances 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 239000002828 fuel tank Substances 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 239000003502 gasoline Substances 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 230000010355 oscillation Effects 0.000 description 1
- 230000002093 peripheral effect Effects 0.000 description 1
- 239000002574 poison Substances 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 230000008092 positive effect Effects 0.000 description 1
- 239000011541 reaction mixture Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 239000004576 sand Substances 0.000 description 1
- 229930195734 saturated hydrocarbon Natural products 0.000 description 1
- 230000007017 scission Effects 0.000 description 1
- 239000013535 sea water Substances 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 238000001228 spectrum Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G19/00—Refining hydrocarbon oils in the absence of hydrogen, by alkaline treatment
- C10G19/073—Refining hydrocarbon oils in the absence of hydrogen, by alkaline treatment with solid alkaline material
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G29/00—Refining of hydrocarbon oils, in the absence of hydrogen, with other chemicals
- C10G29/04—Metals, or metals deposited on a carrier
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
- C10G67/10—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including alkaline treatment as the refining step in the absence of hydrogen
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
- C10G2300/202—Heteroatoms content, i.e. S, N, O, P
Definitions
- the invention relates to a process for the desulfurization of a hydrocarbon mixture containing organic sulfur compounds.
- the desulphurization of hydrocarbon mixtures plays an important role in the art mainly because sulfur is a so-called "catalyst poison" and the exceeding of a certain limit by the sulfur content makes a hydrocarbon mixture unusable for a variety of possible uses more stringent legislation, which provides for maximum levels of sulfur even in applications where the hydrocarbons are only burned on a regular basis, in particular to reduce the sulfur content of the resulting exhaust gases.
- a disadvantage of this method is that with decreasing sulfur content of the hydrogen demand for the removal of sulfur increases disproportionately to the removed amount of sulfur. This is because some of the sulfur compounds are more reactive than others in terms of the chemical reactions involved in hydrodesulfurization. At the same time, however, other side reactions occur in which hydrogen is consumed. Examples include the conversion of unsaturated into saturated hydrocarbons or the cleavage of hydrocarbons to form hydrocarbons with a higher hydrogen / carbon ratio. Accordingly, the costs for hydrodesulfurization increase disproportionately in the attempt to achieve the lowest possible residual sulfur contents in the hydrocarbon mixture.
- GB 759283 A discloses a process in which a sodium dispersion is used to desulphurise a hydrocarbon mixture in an autoclave. It has been shown that it is possible in this way to remove sulfur from the hydrocarbon mixture, but the residual sulfur content obtained are still above the sulfur content, which is regularly required today.
- the invention is therefore based on the object to show a desulfurization of the type mentioned, which can be realized meaningful on an industrial scale.
- the object is achieved by a process for the desulfurization of a hydrocarbon mixture containing organic sulfur compounds, comprising the following steps: a) preparing a sodium dispersion b) adding the sodium dispersion to the hydrocarbon mixture to be desulfurized c) passing the mixture of sodium dispersion and hydrocarbon mixture through a reactor, wherein the Reaction conditions, in particular pressure and temperature are chosen so that there is a reaction of the sodium with the organic sulfur compounds, wherein the sulfur atoms are dissolved out of the organic sulfur compounds and combine with the sodium, wherein the reactor is a turbulent flow reactor, preferably a tubular reactor or an oscillating plug reactor with internal screw conveyor, according to claim 1.
- the reactor is a turbulent flow reactor, preferably a tubular reactor or an oscillating plug reactor with internal screw conveyor, according to claim 1.
- the object is achieved in that the reactor in which the reaction takes place, a turbulent flow through reactor, preferably a tubular reactor is.
- a propulsion reactor having an internal oscillating driven screw conveyor, in which it is ensured by appropriate technical devices that a turbulent flow is created and the design ensures a sufficient residence time of the hydrocarbon mixture to be desulphurized. It has been shown that in a reactor, preferably a tubular reactor or a propene reactor, with turbulent flow, the reaction parameters can be adjusted so that when passing a mixture of a sodium dispersion and a hydrocarbon mixture through this reactor an extremely low residual sulfur content can be achieved.
- residual sulfur content is based on the sulfur, which is still present in the form of organic sulfur compounds after carrying out the reaction, it is understood that for the final removal of sulfur by the sodium, in particular inorganic, preferably in the form of Na 2 S, bound sulfur must still be separated with the sodium from the mixture.For this purpose, a number of known from the prior art separation methods are available.
- the tubular reactor Due to the turbulent flow in the reactor, preferably in the tubular reactor or in the grafting reactor, a sufficient mixing of the reaction mixture can be generated in order to carry out the reaction until reaching low residual sulfur contents, so as to ensure economical desulfurization. It is particularly advantageous in this context if the tubular reactor has a corresponding length for this purpose. This is preferably at least 100 m, more preferably at least 200 m. It has been found that at these very high tube lengths suitable flow conditions with a corresponding sufficient residence time can be realized in order to successfully carry out the process on an industrial scale.
- the tube of the tubular reactor by no means has to be straight, it may rather have a meandering, wound or similar course, in particular in order to enable a space-saving construction of the reactor.
- the reaction tube of the tubular reactor can of course be composed of a plurality of tubes.
- the length of the tubular reactor is therefore to be regarded as the effective length of the flow path through the tube reactor, which is covered by the medium flowing through, in the mixture of sodium dispersion and hydrocarbon mixture, under reaction conditions.
- the propene reactor is ensured by appropriate technical devices, such as the oscillating drive, the turbulent flow and the residence time, and if necessary by the speed control of the screw conveyor and / or the duration of the oscillations regulated.
- the reactor may advantageously have internals for promoting thorough mixing. Such internals are helpful to ensure a turbulent flow and the concomitant the reaction rate conducive mixing.
- the reactor may particularly preferably have so-called static mixers, that is to say stationary components which due to their geometry influence the flow accordingly.
- the temperature in the reactor at least 250 D C, preferably at least 280 ° C. Furthermore, it is advantageous if the temperature in the reactor does not exceed 310.degree. It has been found that particularly favorable conditions for the desired chemical reactions are present in this temperature range.
- volume equivalent spherical diameter of at least 80%, preferably of at least 90% of the sodium particles in the dispersion is at most 25 ⁇ , preferably at most 12 pm and more preferably at most 5 pm. It has been found that a sodium dispersion which is both very fine and has the narrowest possible spectrum of particle distribution is particularly advantageous in terms of the reaction rate.
- the volume equivalent ball diameter of a Sodium particle is the diameter that a spherical sodium particle of the same volume would have. Due to the low melting point of sodium, this is regularly in liquid form at reaction conditions, whereby the sodium particles actually form a spherical shape.
- the volume-equivalent spherical diameter offers a clear characterization of the particle size in the suspension. It is also particularly advantageous if at least 90%, preferably at least 95% of the sodium particles have a volume-equivalent spherical diameter which is less than 5 ⁇ .
- At least 0.05% by weight of sodium particularly preferably at least 0.1% by weight of sodium and particularly preferably at least 1.5% by weight of sodium, based on the total weight of the hydrocarbon mixture to be desulphurized, are preferred in the desulfurization process, used.
- the preparation of the sodium dispersion according to the rotor-stator principle has proven to be particularly advantageous with regard to the process according to the invention.
- dispersing devices are used in which the dispersion is produced by a relative movement between a rotor and a stator with a high peripheral speed. It has been found that sodium dispersions prepared by such a dispersion process in particular have very narrow particle size distributions and are particularly suitable for the process according to the invention.
- the sodium is dispersed in an oil to prepare the sodium dispersion, which may be a paraffinic white oil in a particularly advantageous manner. It has been found that dispersions of sodium in such liquid phases are particularly advantageous for the process according to the invention.
- Particularly high degrees of desulfurization can be achieved, in particular, if the proportion of sodium in the dispersion is from 1 to 40% by weight, preferably from 10 to 33% by weight, based on the total weight of the dispersion. It is particularly advantageous for the desulfurization, when 1 to 40 wt .-% of sodium are dispersed in oil, and preferably at least 80% of the sodium particles is a volume equivalent Have ball diameter smaller than 25 ⁇ im. It is further preferred if 10 to 33% by weight of sodium are dispersed in white oil and preferably at least 90% of the sodium particles have a volume-equivalent spherical diameter which is less than 12 ⁇ m, preferably less than 5 ⁇ m. Under the above conditions, the best desulphurisation results can be achieved.
- the liquid phase used to disperse the sodium has a viscosity of at least 4 mm 2 / s, more preferably at least 12 mm 2 / s, and / or at most 20 mm 2 / s, most preferably at most 17 mn Vs.
- the density of the liquid phase used for the dispersion is preferably at least 0.84 kg / l and or at most 0.89 kg / l. Furthermore, it has been found to be advantageous if the liquid phase used for dispersing the sodium has a flash point of at least 150 ° C, preferably at least 200 ° C.
- the hydrocarbon mixture to be desulphurised is first treated for the purpose of presulfurization with a further desulphurization process. Later, desulfurization is then carried out by treatment with a desulfurization process according to the invention.
- This process procedure has the advantage that the advantages of conventional desulphurization processes, in particular hydrogenating desulphurization processes, can be combined with the advantages of desulfurization with a sodium dispersion. It makes sense initially to remove that part of the sulfur which can still be removed comparatively well with a hydrogenating desulphurization process. As a result, most of the sulfur is already removed. The sodium dispersion-based process is then used to lower the residual sulfur content even further.
- the part of the sulfur is removed, which is very difficult to remove with the hydrogenating desulfurization, although in such a procedure, a total of only a very small portion of the total sulfur is removed by the sodium dispersion, so the overall efficiency of the combined process is significantly increased, because the desulfurization by means of the sodium dispersion is used exactly where it the is economically superior to hydrodesulfurization, namely when very low levels of sulfur are reached.
- the advantages of the hydrodesulphurisation process can be utilized in the removal of comparatively large amounts of sulfur up to a moderate residual sulfur content.
- the desulfurization by means of the sodium dispersion does not have to be directly and directly connected to the preferably hydrodesulfurizing desulfurization. It is quite possible to subject the hydrocarbon mixture formed in the meantime to further process steps, to separate off parts of the hydrocarbon mixture or to mix the hydrocarbon mixture with other substances, in particular other hydrocarbon mixtures. Incidentally, this also applies to the sequence between the dispersion preparation and the addition of the sodium dispersion to the hydrocarbon mixture to be desulphurised.
- the process variants described above for the preparation of the sodium dispersion have the advantage that the sodium dispersion is correspondingly stable, i. it can easily be stored or transported between production facilities before it is added to the hydrocarbon mixture.
- a further particularly advantageous procedure provides that the hydrocarbon mixture to be desulphurised is a fuel or a fraction of a hydrocarbon mixture intended for further processing into a fuel.
- mineral oil fractions for concrete later uses for example the production of diesel fuels - are separated early on and processed further in different process paths.
- the fractions used for the use of diesel and / or gasoline fuels have a certain proportion of low-boiling components.
- the pressure in the reactor is at least 6 bar, preferably at least 8 bar. In this way, a safe implementation and especially light boiling components in the liquid phase can take place.
- the pressure in the reactor is at most 3 bar, preferably at most 1.5 bar.
- These Process variant is particularly advantageous if the proportion of low boilers in the hydrocarbon mixture is low. Such an operation is particularly advantageous when comparatively small and compact systems can be used. Due to the low pressure, the material stresses decrease, especially the comparatively long tube reactors can be made much thinner, which has a very positive effect in terms of size and weight of the system.
- the process according to the invention can be used particularly advantageously in the desulfurization of hydrocarbon mixtures which originate from a liquefaction process for obtaining liquid hydrocarbons from solids.
- Such methods find particular use when liquid hydrocarbon mixtures are to be recovered from waste for use as fuels or fuels.
- Low-boiling constituents often play a subordinate role in these mixtures, whereas the possibility of constructing cost-effective and / or compact plants often represents a considerable economic advantage.
- Slop Oil is a contaminated, mineral oil-containing mixture, which is obtained, for example, and in particular when rinsing tanks on ships. These can be, for example, the tanks of mineral oil tankers, but also fuel tanks of ships fueled in particular with heavy oil. Regular cooling circuits and the like on such ships, especially in the field of marine engines, not fully sealed, so that seawater and other contaminants to the marine life and the like in the tanks in question penetrate and in the tanks so as to form the so-called slop oil difficult to recycle.
- a hydrocarbon mixture 1 derived, for example, from a liquefaction process for the recovery of liquid hydrocarbons or a treatment process from slop oil (or a mixture thereof).
- sodium 2 is dispersed with an oil 3 in the example shown in a method step S1.
- a dispersion according to the rotor-stator principle is used.
- a paraffinic white oil is used as oil 1.
- the sodium dispersion which has been prepared in step S1 and the hydrocarbon mixture 1 are mixed.
- the reaction step S3 is preferably in a tubular reactor at turbulent
- the tubular reactor preferably has a length of at least 200m.
- the reactor can be designed, for example, a shaped.
- the use of an oscillating plug-in reactor with internal transport screw is advantageous.
- At an advantageous reaction temperature between 280 ° C and 310 ° C occurs in the reactor during the process step S3 to the process of the invention underlying chemical reactions in which the sulfur is dissolved out of the organic sulfur compounds and reacts to inorganic sulfur compounds, in particular to a2S.
- the desulfurized hydrocarbon product 4 separates the inorganic sulfur-containing constituents formed by the process according to the invention, in particular the Na2S5.
Abstract
Description
Claims
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
PL17720561T PL3417035T3 (pl) | 2016-02-19 | 2017-02-13 | Sposób odsiarczania mieszaniny węglowodorów |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE102016102933.5A DE102016102933A1 (de) | 2016-02-19 | 2016-02-19 | Verfahren zur Entschwefelung eines Kohlenwasserstoffgemisches |
PCT/IB2017/000101 WO2017141097A1 (de) | 2016-02-19 | 2017-02-13 | Verfahren zur entschwefelung eines kohlenwasserstoffgemisches |
Publications (2)
Publication Number | Publication Date |
---|---|
EP3417035A1 true EP3417035A1 (de) | 2018-12-26 |
EP3417035B1 EP3417035B1 (de) | 2020-07-29 |
Family
ID=58645325
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP17720561.4A Active EP3417035B1 (de) | 2016-02-19 | 2017-02-13 | Verfahren zur entschwefelung eines kohlenwasserstoffgemisches |
Country Status (5)
Country | Link |
---|---|
EP (1) | EP3417035B1 (de) |
DE (1) | DE102016102933A1 (de) |
DK (1) | DK3417035T3 (de) |
PL (1) | PL3417035T3 (de) |
WO (1) | WO2017141097A1 (de) |
Family Cites Families (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB759283A (en) | 1952-12-24 | 1956-10-17 | British Petroleum Co | Improvements relating to the refining of petroleum hydrocarbons |
WO2008106402A2 (en) * | 2007-02-26 | 2008-09-04 | Trans Ionics Corporation | Desulfurization of petroleum streams using metallic sodium |
US7527724B1 (en) * | 2005-11-17 | 2009-05-05 | Trans Ionics Corporation | Process for desulfurization of hydrocarbons |
-
2016
- 2016-02-19 DE DE102016102933.5A patent/DE102016102933A1/de not_active Withdrawn
-
2017
- 2017-02-13 WO PCT/IB2017/000101 patent/WO2017141097A1/de active Application Filing
- 2017-02-13 PL PL17720561T patent/PL3417035T3/pl unknown
- 2017-02-13 DK DK17720561.4T patent/DK3417035T3/da active
- 2017-02-13 EP EP17720561.4A patent/EP3417035B1/de active Active
Also Published As
Publication number | Publication date |
---|---|
WO2017141097A1 (de) | 2017-08-24 |
DK3417035T3 (da) | 2020-10-12 |
EP3417035B1 (de) | 2020-07-29 |
DE102016102933A1 (de) | 2017-08-24 |
PL3417035T3 (pl) | 2021-01-25 |
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